邻苯二甲酸二辛酯生产车间初步工艺设计论文

题目：年产8万吨邻苯二甲酸二辛酯生产车间初步工艺设计的通用增H2438424384continuousesterificationtechnology,thecaThedesignfollowsthe"maturetechnology,advancedtechnology,equipmentconfigurationscientific,environmentalprocessandequipmentcphthalicanhydrideandiso-octanolafteresterification,defacilitiesandprocessselection,withaflowchartwithcontrolreductionofthe"threewastwastes"treatment,toensuresafeprodKeyword:DOPEthylhexanolPhthalicProcessDesign 7 7 7 7 7 82令设计的目的和意义 8 8 8 8 9 9 9 9 10 10 11 11 11 12 12 13 13 13 14 14 14 16 17 18 19 19 20 20 21 22 23 23 23 23 23 24 25 26 27 28 28 28 29 29 30 31 31 31 31 31 31 35令1令在学习掌握所学的化学工艺学、化工机械设备基础、化工原理等课程的3令项目设计依据和原则令1令按技术先进、成熟可靠、经济合理的原则对技术方案进行论证令以确定最令2令尽可能采用节能工艺和高效设备令充分发挥规模效应令降低能耗、物耗和令3令考虑“三废”治理和综合利用副产物令充分重视环保防污、科学生产、生令1令工艺生产方法确定、生产流程设计与论证令2令工艺计算令包括物料衡算令热量衡算令令5令设计绘图酸度令以对苯二甲酯计令%≤体积电阻率令×10?.m≥优级品一级品合格品透明液体令无悬浮物99.099.5099.500.981令0.9860.01520.0200.2512aOH设测定回流比为2.5令设回流异辛醇量Xkmol则出釜异辛醇为2.5Xkmol2水表4令一级酯化段物料衡算表量令kmol/h令26.9680.8600066.6733.33令%令令%令量令kmol/h令53.9026.960.320.3221600C/kJ/(mol.k)0.28560.2559C/kJ/(mol.k)C0.28290.5347/()0.4935J/mol-373.2邻苯二甲酸一辛酯0.45230..34540.31550.2694-672.6-1120.6注令A------苯酐令B-----异辛醇;C------邻苯二甲酸一辛酯A=nACp,mAΔT=10.12×269.4×[(150−30)+273.15]=1.072×10kJ6Q=nCΔT=32.05ΔH=q6A(l令423.15K)+B(l,423.15K)ΔH7C(ΔHΔΔHΔHΔHΔΔH=nCΔT=−10.12×269.4×(423.15−404.75)=ΔH=nΔH=nCΔT=−32.05×311.5×(423.15−298.15)=−1.248×106ΔH=n(ΔfHm−ΔH−ΔH)=10.12(−1120.6+672.6+373.ΔH=nΔCΔT=10.12×493.5×(423.15−298.15)=0.6246所以令ΔH=ΔH+ΔH+ΔH+ΔH+ΔH+ΔH=−1.73×10kJ/h2p00.7960.121553995.2504.5055.2953723.124104.18200.746液体比热容KJ/(kg.℃)61.992.2941031513.6水40.694.1785.29215250.122AAV=Qt令1+η令3316-11 =1.005g/m3W=1.005×1×9.81×2.43+0.1015×1000000=0.125MPa2cd=1.46mm+2mmd1低粘度混合○≤0.9Φσ有令0.9Φσs=0.9×1.0×200M= T搅拌器环粘涡式桨式推式折叶开涡轮式流动状态○○○○○○○度液传热○○搅拌目的搅拌容转速X)最高度OOOOO0O00布尔马金式锚式螺杆式螺带式OO1令100300OOOOOOOOOO注令有O者为合用令空白者不详或不合用。轮式搅拌器。由《化工原理》上册教材中表4ibp6.3x1.005x1.2x03.73x100=2268Wpj44j=0.11×0.76×10/.2=380W/(m.Co/Dc))λ/De3ecRe=Duρ/µ=0.4×0.78×992.2/0.000656=0.47×10e5(60.8-50.334α=55.38×63.38/0.4=8775.1W/(m.C)2om设计计算数据及选型设计计算数据及选型六片平直叶圆盘涡轮式搅拌器0.2mdc器搅拌桨叶数搅拌功率挡板数挡板宽度搅拌釜全容积令不包括封头部分令液面深度搅拌釜实际高度搅拌釜内经工作压力搅拌釜厚度夹套形式螺旋板螺距夹套环隙夹套内冷却水流速冷却水每小时移出热量被搅拌液体侧的对流传热系数zNnbwVhHDiPTδnPEuQ663螺旋板夹套α8775.1W/(m2.α8775.1W/(m2.oC)370.4W/(m.C)370.4W/(m.C)0065)(7025)Δ=初步假设采用单壳程令偶数管的固定板换热器经查表Ψ=0.88>0.8所以假设可行令采用单壳程令偶数管的固定板换热器Δtm=ΨΔtm逆=0.88x72.4=63.7℃ΔTm令=515.18/令63.7x370.4令=21.83m2公称面积令㎡令0.0083管子尺寸令mm令25x2.5pT管子排列方式正三角形/N=π/4x0.02x2106/4100000025510−34ix0xx230.02ΔPix230.02ΔPi=(λx20+)fNi0.8u2i2ix(223.9x0.35x10-)30.312.)iild∴i3600ρ0S03600x992.2x0.01333πd0π×0.025且4x0.000656cμ4.==4.32x1005cμ4.3 00.55)00.55=令=所以1.OR0μμ1=0.36x0.0202x8250x0.0000432x1.05=6135.53W/(m2.C)令0.553′0B-0.190ΔP0x190.45x(22+1)=1.72x8250-0.19u2×u2×00.41xx=0=7.6.41xx=0=7.6x1022③计算传热面积=++KK令忽略管壁热阻令则=计Q=K 97x6A=A=计ii